Alumina Guard Bed for Aromatics Transalkylation Process

ABSTRACT

A transalkylation process for reacting carbon number nine aromatics with toluene to form carbon number eight aromatics such as para-xylene is herein disclosed. The process is based on the discovery that deactivating contaminants present in typical hydrocarbon feeds, such as chlorides, can be removed with an alumina guard bed prior to contacting with a transalkylation catalyst. Effective transalkylation catalysts have a solid-acid component such as mordenite, and a metal component such as rhenium. The invention is embodied in a process, a catalyst system, and an apparatus. The invention provides for longer catalyst cycle life when processing aromatics under commercial transalkylation conditions.

CROSS-REFERENCE TO RELATED APPLICATION

This application is a Division of copending application Ser. No.10/946,948 filed Sep. 22, 2004, the contents of which are herebyincorporated by reference in its entirety.

FIELD OF THE INVENTION

This invention relates to catalytic hydrocarbon conversion, and morespecifically to the use of an activated alumina guard bed for extendingthe life of a transalkylation catalyst used in reacting aromatic C₉+compounds with toluene to produce xylenes. By decomposing contaminantspecies present in transalkylation feed aromatics, such as chlorides,the guard bed reduces coke formation on the transalkylation catalyst.

BACKGROUND OF THE INVENTION

Xylene isomers, para-xylene, meta-xylene and ortho-xylene, are importantintermediates which find wide and varied application in chemicalsyntheses. Para-xylene upon oxidation yields terephthalic acid, which isused in the manufacture of synthetic textile fibers and resins.Meta-xylene is used in the manufacture of plasticizers, azo dyes, woodpreservers, etc. Ortho-xylene is feedstock for phthalic anhydrideproduction.

Xylene isomers from catalytic reforming or other sources generally donot match demand proportions as chemical intermediates, and furthercomprise ethylbenzene, which is difficult to separate or to convert.Para-xylene in particular is a major chemical intermediate with rapidlygrowing demand, but amounts to only 20 to 25% of a typical C₈ aromaticsstream. Among the aromatic hydrocarbons, the overall importance of thexylenes rivals that of benzene as a feedstock for industrial chemicals.Neither the xylenes nor benzene are produced from petroleum by thereforming of naphtha in sufficient volume to meet demand, and conversionof other hydrocarbons is necessary to increase the yield of xylenes andbenzene. Often toluene (C₇) is dealkylated to produce benzene (C₆) orselectively disproportionated to yield benzene and C₈ aromatics fromwhich the individual xylene isomers are recovered.

A current objective of many aromatics complexes is to increase the yieldof xylenes and to de-emphasize benzene production. Demand is growingfaster for xylene derivatives than for benzene derivatives. Refinerymodifications are being effected to reduce the benzene content ofgasoline in industrialized countries, which will increase the supply ofbenzene available to meet demand. A higher yield of xylenes at theexpense of benzene thus is a favorable objective, and processes totransalkylate C₉ and heavier aromatics with benzene and toluene havebeen commercialized to obtain high xylene yields.

U.S. Pat. No. 4,857,666 discloses a transalkylation process overmordenite and incorporating a metal modifier into the catalyst.

U.S. Pat. No. 5,763,720 discloses a transalkylation process forconversion of C₉+ into mixed xylenes and C₁₀+ aromatics over a catalystcontaining zeolites including amorphous silica-alumina, MCM-22, ZSM-12,and zeolite beta, where the catalyst further contains a Group VIII metalsuch as platinum.

U.S. Pat. No. 6,060,417 discloses a transalkylation process using acatalyst based on mordenite with a particular zeolitic particle diameterand having a feed stream limited to a specific amount of ethylcontaining heavy aromatics. The catalyst contains nickel or rheniummetal.

U.S. Pat. No. 6,486,372 B1 discloses a transalkylation process using acatalyst based on dealuminated mordenite with a high silica to aluminaratio that also contains at least one metal component.

U.S. Pat. No. 6,613,709 B1 discloses a catalyst for transalkylationcomprising zeolite structure type NES and metals such as rhenium,indium, or tin.

U.S. Pat. No. 6,740,788 B1 discloses an integrated process for aromaticsproduction enabled by a stabilized transalkylation catalyst having ametal function.

Many types of supports and elements have been disclosed for use ascatalysts in processes to transalkylate various types of aromatics intoxylenes, but there exists a problem presented by transalkylationaromatics feed stream contaminants, whereby such contaminants reduce theuseful catalyst cycle life. Applicants have found a solution with theapplication of a contaminant removal guard bed that extends catalystlife, resulting in a more stable aromatics transalkylation process thatwill be more profitable over the catalyst life cycle by requiring lessfrequent down time for regeneration to remove deactivating cokedeposits.

SUMMARY OF THE INVENTION

A principal object of the present invention is to provide a process ofusing a guard bed in front of a transalkylation catalyst, the guard bedcatalyst system itself, and a reactor configuration for thetransalkylation of alkylaromatic hydrocarbons into xylenes. Morespecifically, the present invention is directed to improved conversionof aromatic hydrocarbons by removal of feed contaminants. This inventionis based on the discovery that feed contaminants removed in a guard bedprior to contacting the feed with a transalkylation catalystdemonstrates a process showing increased stability of xylene productionunder transalkylation conditions.

Accordingly, a broad embodiment of the present invention is a processfor contacting an aromatics stream containing a contaminant materialwith a guard bed and then with a catalyst suitable for transalkylationof the aromatics into xylenes. In another embodiment, the presentinvention is a catalyst system combining guard bed material withcatalyst material. In yet another embodiment, the present invention is areactor configuration providing an apparatus for situating a guard bedbefore a catalyst bed.

These, as well as other objects and embodiments will become evident fromthe following detailed description of the invention.

BRIEF DESCRIPTION OF THE DRAWING

The FIGURE shows the effect of guard bed addition upon catalyst activityfor transalkylation of C₇, C₉, and C₁₀ aromatics at a level of about 50wt-% conversion while producing C₈ aromatics. The slope of the weightedaverage catalyst bed temperature (WABT) is proportional to stability,with a flatter slope representing greater stability.

DETAILED DESCRIPTION OF THE INVENTION

The feed stream to the present process generally comprises alkylaromatichydrocarbons of the general formula C₆H_((6-n))R_(n), where n is aninteger from 0 to 6 and R is CH₃, C₂H₅, C₃H₇, or C₄H₉, in anycombination. Suitable alkylaromatic hydrocarbons include, for examplebut without so limiting the invention, benzene, toluene, ethylbenzene,ethyltoluenes, propylbenzenes, tetramethylbenzenes,ethyl-dimethylbenzenes, diethylbenzenes, methylpropylbenzenes,ethylpropylbenzenes, triethylbenzenes, di-isopropylbenzenes, andmixtures thereof. The feed stream may comprise lower levels ofortho-xylene, meta-xylene, and para-xylene that are the desired productsof the present process.

The feed stream also may comprise naphthalene and other C₁₀ and C₁₁aromatics and suitably is derived from one or a variety of sources.Polycyclic aromatics such as the bi-cyclic components includingnaphthalene, methylnaphthalene, are permitted in the feed stream of thepresent invention. Indane, which is also referred to as indan or indene,is meant to define a carbon number nine aromatic species with one carbonsix ring and one carbon five ring wherein two carbon atoms are shared.Naphthalene is meant to define a carbon number ten aromatic species withtwo carbon six rings wherein two carbon atoms are shared. Polycyclicaromatics may also be present, even in substantial amounts such asgreater than about 0.5 wt-% of the feed stream.

Feed components may be produced synthetically, for example, from naphthaby catalytic reforming or by pyrolysis followed by hydrotreating toyield an aromatics-rich product. The feed stream may be derived fromsuch product with suitable purity by extraction of aromatic hydrocarbonsfrom a mixture of aromatic and nonaromatic hydrocarbons andfractionation of the extract. For instance, aromatics may be recoveredfrom reformate. Reformate may be produced by any of the processes knownin the art. The aromatics then may be recovered from reformate with theuse of a selective solvent, such as one of the sulfolane type, in aliquid-liquid extraction zone. The recovered aromatics may then beseparated into streams having the desired carbon number range byfractionation. When the severity of reforming or pyrolysis issufficiently high, extraction may be unnecessary and fractionation maybe sufficient to prepare the feed stream. Such fractionation typicallyincludes at least one separation column to control feed end point.

The feed heavy-aromatics stream, characterized by C₉+ aromatics (orA₉+), permits effective transalkylation of light aromatics such asbenzene and toluene with the heavier C₉+ aromatics to yield additionalC₈ aromatics that are preferably xylenes. The heavy-aromatics streampreferably comprises at least about 90 wt-% total aromatics; and may bederived from the same or different known refinery and petrochemicalprocesses as the benzene and toluene, and/or may be recycled from theseparation of the product from transalkylation. When the feed ispredominantly heavy-aromatics then de-alkylation or hydrocracking of theheavy aromatics to lighter aromatics may also occur and provideadditional intermediate feed components that may further convert tobenzene, toluene or xylene.

Feed contaminants may be present in small amounts, such as amounts lessthan 100 wt-ppm, and more generally are present in amounts less than 10wt-ppm. Feed contaminants include, but are not limited to, oxygen,chloride, sulfur, and nitrogen species.

According to the process of the present invention, the feed mixture ofheavy A₉+, toluene, and feed contaminants is contacted with an aluminaguard bed and then with a transalkylation catalyst of the typehereinafter described in a two zone system. The first zone is the guardbed zone, while the second zone is the transalkylation zone. The guardbed may be contained in a separate vessel from the transalkylationreactor of the types hereinafter described, or it may be containedwithin the same reactor vessel as the transalkylation catalyst. Betterflow distribution is achieved when catalyst support materials, forexample inert ceramic objects, are placed in upstream and downstreampositions from the alumina guard bed material. Therefore, when the twozones are placed in separate vessels appropriate piping is used toserially connect them together. When the two zones are in the samevessel, then the zones are generally layered on top or next to eachother such that contacting with hydrocarbons occurs sequentially andunder the same conditions. Alternatively, the zones may be intermixed,such that physical mixtures of guard bed and transalkylation particlesare combined together on a bulk basis where separate particles areintermingled, or on a particulate basis where effective guard bedmaterial is directly composited alongside catalyst material. Finally,such zones are herein described as in fluid communication with eachother by being present in the same vessel, or connected in series withseparate vessels and piping there between for transference of thealumina guard bed product to the transalkylation reactor.

The hydrocarbon feed is passed through an alumina guard bed and producesan alumina guard bed product stream. The alumina guard bed productstream is then preferably transalkylated in the vapor phase and in thepresence of hydrogen. If transalkylated in the liquid phase, then thepresence of hydrogen is optional. If present, free hydrogen isassociated with the feed stream and recycled hydrocarbons in an amountof from about 0.1 moles per mole of alkylaromatics up to 10 moles permole of alkylaromatic. This ratio of hydrogen to alkylaromatic is alsoreferred to as hydrogen to hydrocarbon ratio. The transalkylationreaction preferably yields a product having increased xylene content.

The feed to alumina guard bed zone usually first is heated by indirectheat exchange against the effluent of the transalkylation reaction zoneand then is heated to reaction temperature by exchange with a warmerstream, steam or a furnace. The feed then is passed through the guardbed zone and then through a reaction zone, which may comprise one ormore individual reactors. The use of a single transalkylation reactionvessel having a fixed cylindrical bed of catalyst is preferred, butother reaction configurations utilizing moving beds of catalyst orradial-flow reactors may be employed if desired. Passage of the combinedfeed through the reaction zone effects the production of an effluentstream comprising unconverted feed and product hydrocarbons including C₈aromatic compounds. This effluent is normally cooled by indirect heatexchange against the stream entering the reaction zone and then furthercooled through the use of air or cooling water. The effluent may bepassed into a stripping column in which substantially all C₅ and lighterhydrocarbons present in the effluent are concentrated into an overheadstream and removed from the process. An aromatics-rich stream isrecovered as net stripper bottoms, which is referred to herein as thetransalkylation effluent.

To effect a transalkylation reaction, the present invention incorporatesa transalkylation catalyst in at least one zone, but no limitation isintended in regard to a specific catalyst other than such catalyst mustpossess a solid-acid component and a metal component. Conditionsemployed in the transalkylation zone normally include a temperature offrom about 200° to about 540° C. The transalkylation zone is operated atmoderately elevated pressures broadly ranging from about 100 kPa toabout 6 MPa absolute. The transalkylation reaction can be effected overa wide range of space velocities. Weight hourly space velocity (WHSV)generally is in the range of from about 0.1 to about 20 hr⁻¹. Suchtransalkylation conditions are similar to the alumina guard bedconditions.

The transalkylation effluent is separated into a light recycle stream, amixed C₈ aromatics product and a heavy recycle stream. The mixed C₈aromatics product can be sent for recovery of para-xylene and othervaluable isomers. The light recycle stream may be diverted to other usessuch as to benzene and toluene recovery, but alternatively is recycledpartially to the transalkylation zone or the alumina guard bed zone. Theheavy recycle stream contains substantially all of the C₉ and heavieraromatics and may be partially or totally recycled to thetransalkylation reaction zone or the alumina guard bed zone as well.

Several types of alumina guard bed materials may be used in the presentinvention including gamma alumina, theta alumina, and other aluminaphase materials having high surface areas generally greater than about25 m²/g, with gamma phase alumina being preferred. Alpha phase aluminagenerally has a low surface area is not generally suitable for thepresent invention. Gamma phase alumina is obtained by aging andcalcining aluminum trihydroxides [Al(OH)₃], aluminum oxyhydroxides[AlOOH], transition aluminas derived from Al(OH)₃ and AlOOH, and,optionally metal promoters with any combination thereof. Generally,alumina will be precipitated from an aqueous solution containing Al+3ions. Such precipitate is aged, filtered, washed and dried. During theseoperations alumina passes through various phases. Typically, the initialprecipitation leads to a gel with minute crystals of boehmite. The gelcan be aged at a temperature of about 80° C. into crystalline boehmitethat forms gamma-phase alumina upon a calcination temperature of about600° C. Gamma phase alumina has a high surface area, generally between100 and 300 m²/g. Upon heating to higher temperatures of about 1100° C.or more, the alumina moves through theta or delta phases to becomesalpha phase and has a low surface area less than 25 m²/g and commonlyless than 1 m²/g.

Several types of transalkylation catalysts that may be used in thepresent invention are based on a solid-acid material combined with anoptional metal component. Suitable solid-acid materials include allforms and types of mordenite, mazzite (omega zeolite), beta zeolite,ZSM-11, ZSM-12, ZSM-22, ZSM-23, MFI type zeolite, NES type zeolite,EU-1, MAPO-36, MAPSO-31, SAPO-5, SAPO-11, SAPO-41, and silica-alumina orion exchanged versions of such solid-acids. For example, in U.S. Pat.No. 3,849,340 a catalytic composite is described comprising a mordenitecomponent having a SiO₂/Al₂O₃ mole ratio of at least 40:1 prepared byacid extracting Al₂O₃ from mordenite prepared with an initial SiO₂/Al₂O₃mole ratio of less than 30:1 and a metal component selected from copper,silver and zirconium. Refractory inorganic oxides, combined with theabove-mentioned and other known catalytic materials, have been founduseful in transalkylation operations. For instance, silica-alumina isdescribed in U.S. Pat. No. 5,763,720. Crystalline aluminosilicates havealso been employed in the art as transalkylation catalysts. ZSM-12 ismore particularly described in U.S. Pat. No. 3,832,449. Zeolite beta ismore particularly described in Re. 28,341 (of original U.S. Pat. No.3,308,069). A favored form of zeolite beta is described in U.S. Pat. No.5,723,710, which is incorporated herein by reference. The preparation ofMFI topology zeolite is also well known in the art. In one method, thezeolite is prepared by crystallizing a mixture containing an aluminasource, a silica source, an alkali metal source, water and an alkylammonium compound or its precursor. Further descriptions are in U.S.Pat. No. 4,159,282, U.S. Pat. No. 4,163,018, and U.S. Pat. No.4,278,565. The synthesis of the Zeolite Omega is described in U.S. Pat.No. 4,241,036. ZSM intermediate pore size zeolites useful in thisinvention include ZSM-5 (U.S. Pat. No. 3,702,886); ZSM-11 (U.S. Pat. No.3,709,979); ZSM-12 (U.S. Pat. No. 3,832,449); ZSM-22 (U.S. Pat. No.4,556,477); ZSM-23 (U.S. Pat. No. 4,076,842). European Patent EP 0378916B1 describes NES type zeolite and a method for preparing NU-87. The EUOstructural-type EU-1 zeolite is described in U.S. Pat. No. 4,537,754.MAPO-36 is described in U.S. Pat. No. 4,567,029.

MAPSO-31 is described in U.S. Pat. No. 5,296,208 and typical SAPOcompositions are described in U.S. Pat. No. 4,440,871 including SAPO-5,SAPO-11 and SAPO-41. Typically, the solid-acid component will be presentin the catalyst in an amount from about 1 to about 99 wt-%.

A refractory binder or matrix is optionally utilized to facilitatefabrication of the catalyst, provide strength and reduce fabricationcosts. The binder should be uniform in composition and relativelyrefractory to the conditions used in the process. Suitable bindersinclude inorganic oxides such as one or more of alumina, magnesia,zirconia, chromia, titania, boria, thoria, phosphate, zinc oxide andsilica. Alumina is a preferred binder. Typically the binder may bepresent in about 5 to about 95 wt-% of the catalyst when it is used.

The catalyst also may contain a metal component. One preferred metalcomponent is a Group VIII (IUPAC 8-10) metal that includes nickel, iron,cobalt, and platinum-group metal. Of the platinum group, i.e., platinum,palladium, rhodium, ruthenium, osmium and iridium, platinum isespecially preferred. Another preferred metal component is rhenium andit will be used for the general description that follows. This metalcomponent may exist within the final catalytic composite as a compoundsuch as an oxide, sulfide, halide, or oxyhalide, in chemical combinationwith one or more of the other ingredients of the composite. The rheniummetal component may be incorporated in the catalyst in any suitablemanner, such as coprecipitation, ion-exchange, co-mulling orimpregnation. The preferred method of preparing the catalyst involvesthe utilization of a soluble, decomposable compound of rhenium metal toimpregnate the carrier material in a relatively uniform manner. Typicalrhenium compounds which may be employed include ammonium perrhenate,sodium perrhenate, potassium perrhenate, potassium rhenium oxychloride,potassium hexachlororhenate (IV), rhenium chloride, rhenium heptoxide,perrhenic acid, and the like compounds. Preferably, the compound isammonium perrhenate or perrhenic acid because no extra steps may beneeded to remove any co-contaminant species. This component may bepresent in the final catalyst composite in any amount which iscatalytically effective, generally comprising about 0.01 to about 2 wt-%of the final catalyst calculated on an elemental basis.

The catalyst may optionally contain additional metal components alongwith those metal components discussed above or include additional metalcomponents instead of those metal components in their entirety.Additional metal components of the catalyst include, for example, tin,germanium, lead, and indium and mixtures thereof. Catalyticallyeffective amounts of such additional metal components may beincorporated into the catalyst by any means known in the art. Apreferred amount is a range of about 0.01 to about 2.0 wt-% on anelemental basis.

One shape of the catalyst of the present invention is a cylinder. Suchcylinders can be formed using extrusion methods known to the art.Another shape of the catalyst is one having a trilobal or three-leafclover type of cross section that can be formed by extrusion. Anothershape is a sphere that can be formed using oil-dropping methods or otherforming methods known to the art.

At least one oxidation step may be used in the preparation of thecatalyst. The conditions employed to effect the oxidation step areselected to convert substantially all of the metallic components withinthe catalytic composite to their corresponding oxide form. The oxidationstep typically takes place at a temperature of from about 370° to about650° C. An oxygen atmosphere is employed typically comprising air.Generally, the oxidation step will be carried out for a period of fromabout 0.5 to about 10 hours or more, the exact period of time being thatwhich is required to convert substantially all of the metalliccomponents to their corresponding oxide form. This time will, of course,vary with the oxidation temperature employed and the oxygen content ofthe atmosphere employed.

In preparing the catalyst, a reduction step may be employed. Thereduction step is designed to reduce substantially all of the metalcomponents to the corresponding elemental metallic state and to ensure arelatively uniform and finely divided dispersion of this componentthroughout the catalyst.

Finally, the catalytic composite is subjected to an optional sulfurtreatment or pre-sulfiding step. The sulfur component may beincorporated into the catalyst by any known technique. Any one or acombination of in situ and/or ex situ sulfur treatment methods ispreferred. The resulting catalyst mole ratio of sulfur to rhenium ispreferably from about 0.1 to less than about 1.5.

EXAMPLES

The following examples are presented only to illustrate certain specificembodiments of the invention, and should not be construed to limit thescope of the invention as set forth in the claims. There are manypossible other variations, as those of ordinary skill in the art willrecognize, within the scope of the invention.

Example 1

A transalkylation catalyst comprising mordenite was prepared forcomparative pilot-plant testing by the forming process called extrusion.Typically, 2500 g of a powder blend of 25 wt-% alumina (commerciallyavailable under the trade names CATAPAL B and/or VERSAL 250) and 75 wt-%mordenite (commercially available under the trade name ZEOLYST CBV-21A)was added to a mixer. A solution was prepared using 10 g nitric acid(67.5 wt-% HNO₃) with 220 g deionized water and the solution wasstirred. The solution was added to the powder blend in the mixer, andmulled to make dough suitable for extrusion. The dough was extrudedthrough a die plate to form cylindrically shaped (0.08 cm diameter)extrudate particles. The extrudate particles were calcined at about 565°C. with 15 wt-% steam for 2 hours.

The catalyst was finished using the extrudate particles and anevaporative impregnation with rhenium metal by using an aqueous solutionof ammonium perrhenate (NH₄ReO₄). The impregnated base was calcined inair at 540° C. for 2 hours and resulted in a metal level of 0.15 wt-%rhenium. Next the catalyst was reduced for 12 hours in substantially dryhydrogen at 500° C.

Example 2

The catalyst was tested for aromatics transalkylation ability in a pilotplant using an aromatics feed blend of C₇, C₉, and C₁₀ aromatics todemonstrate effectiveness of using an alumina guard bed to removecontaminant chlorides when producing C₈ aromatics. The feed propertiesare listed in the table below. Feed Wt-% Non Aromatics 0.11 Benzene 0.00Toluene 44.33 Ethylbenzene 0.01 Mixed Xylenes 0.37 Propylbenzene 3.98Ethyltoluene 20.64 Trimethylbenzene 17.90 DEB + C10A 3.74 Ethyl Xylenes5.21 Tetramethylbenzene 1.41 Butylbenzene 0.40 Indane 1.22 C11+ 0.67Total 100.0

Methylene chloride was also present in the feed at an amount of 3.0wt-ppm.

The test consisted of loading a vertical down-flow reactor with 60 cccatalyst located below 240 cc alumina particles. Two types of aluminaparticles were loaded in two different tests. First, a gamma-phasealumina oxide (obtained by calcining crystalline boehmite atapproximately 600° C.) having 185 m²/g surface area was loaded in Run A.Second, commercially available corundum, alpha-phase aluminum oxide with0.83 m²/g surface area was loaded in Run B.

The loaded reactors were contacted with the feed at 2860 kPa abs (400psig) under a space velocity (WHSV) of 4 hr⁻¹ and hydrogen tohydrocarbon ratio (H₂/HC) of 2. A conversion level of about 50 wt-% offeed aromatics was achieved during the initial part of testing. TheFigure shows the effect of guard bed addition upon catalyst activity fortransalkylation of C₇, C₉, and C₁₀ aromatics at a level of about 50 wt-%conversion while producing C₈ aromatics. The slope of the weightedaverage catalyst bed temperature (WABT) is related to stability wherethe flatter slope represents more stable operation and where higherslope represents less stability and increased catalyst deactivation. RunB, with the alpha alumina guard bed, also indicates a time periodwherein the hydrogen to hydrocarbon ratio was increased from 2:1 to 3:1,without approaching the stability of Run A, with the gamma alumina guardbed.

The data showed that the addition of a high surface area gamma phasealumina guard bed improved the stability over a comparable low surfacearea alumina phase guard bed. Even under conditions of increasedhydrogen to hydrocarbon ratio, the stability difference persisted. Aftertesting, the alumina and catalyst chloride contents were analyzed foreach run. Alpha alumina showed about 0.01 wt-% chloride in front of acatalyst that showed about 0.25 wt-% chloride. In contrast, gammaalumina showed approximately 1.2 wt-% chloride in front of a catalystthat showed about 0.01 wt-% chloride. Accordingly, the gamma aluminaguard bed permitted extended operation of an effective transalkylationcatalyst by removing contaminant feed species.

1. A catalyst system comprising a combination of: (a) a guard bedalumina comprising activated alumina having gamma phase; and (b) atransalkylation catalyst comprising a solid-acid component and a metalcomponent.
 2. The catalyst system of claim 1 wherein the transalkylationcatalyst comprises a metal component selected from the group consistingof rhenium, tin, germanium, lead, indium, nickel, platinum, palladiumand mixtures thereof.
 3. The catalyst system of claim 2 wherein thetransalkylation catalyst comprises a metal component selected from thegroup consisting of rhenium and platinum.
 4. The catalyst system ofclaim 3 where in the metal component is rhenium.
 5. The catalyst systemof claim 1 wherein the metal component is present in an amount of about0.01 to about 2 wt-% of the final catalyst calculated on an elementalbasis.
 6. The catalyst system of claim 5 wherein the transalkylationcatalyst further comprises a sulfur component present in an elementalmole ratio of sulfur to metal component from about 0.1 to about 1.5. 7.The catalyst system of claim 1 wherein the activated alumina is furthercharacterized with a surface area of greater than about 25 m²/g.
 8. Thecatalyst system of claim 1 wherein the solid-acid component selectedfrom the group consisting of mordenite, mazzite, zeolite beta, ZSM-11,ZSM-12, ZSM-22, ZSM-23, MFI topology zeolite, NES topology zeolite,EU-1, MAPO-36, MAPSO-31, SAPO-5, SAPO-11, SAPO-41, and silica-aluminaand mixtures thereof.
 9. The catalyst system of claim 8 wherein thesolid-acid component is selected from the group consisting of mordenite,zeolite beta, and MFI topology zeolite.
 10. The catalyst system of claim8 wherein the solid-acid component is mordenite.